Phenol removal in paraxylene recovery process

ABSTRACT

The invention is directed to purification of an aromatic hydrocarbon stream including selective removal of phenol from a process stream comprising aromatic hydrocarbon mixtures, especially aromatic hydrocarbon mixtures that contain higher-than-equilibrium paraxylene, by contact with suitable adsorbents, to provide a product stream having lower concentration of phenol than said process stream.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a divisional of and claims priority to and thebenefit of U.S. patent application Ser. No. 13/875,402, filed May 2,2013, now U.S. Pat. No. 9,012,711, U.S. Provisional Application No.61/681,501, filed Aug. 9, 2012, and U.S. Provisional Application No.61/653,698, filed May 31, 2012, the disclosures of which areincorporated herein by reference in their entirety.

FIELD OF THE INVENTION

The invention relates to removal of phenol from aromatic hydrocarbonmixtures, and more particularly, removal of phenol from aromatichydrocarbon mixtures containing higher than equilibrium paraxyleneconcentrations, and to purification of process streams in the productionof paraxylene by alkylation of benzene and/or toluene with methanoland/or demethylether (DME).

BACKGROUND OF THE INVENTION

Of the aromatic C8 isomers, including the three xylene isomers andethylbenzene, paraxylene is of particularly high value since paraxyleneis useful in the manufacture of synthetic fibers and resins. Refineryand chemical plant streams containing the aromatic C8 isomers typicallycontain, at thermodynamic equilibrium, only about 22-24 wt % paraxylene,based on the weight of the xylene isomers in the stream. Separation ofparaxylene from the other C8 isomers requires superfractionation and/ormultistage refrigeration steps and/or adsorptive separation, all ofwhich are energy intensive. There is a need to provide processes forproducing paraxylene in more efficient ways, such as in higherselectivity than can be obtained from refinery and chemical plantstreams.

One known method for producing paraxylene selectively involves thealkylation of toluene and/or benzene with methanol and/or dimethylether(DME) over a solid acid catalyst. Selectivities to paraxylene in excessof 90 wt % (based on total C₈ aromatic product) have been reported byreacting toluene with methanol in the presence of a catalyst comprisinga porous crystalline material, preferably a medium-pore zeolite andparticularly ZSM-5, having a Diffusion Parameter for 2,2 dimethylbutaneof about 0.1-15 sec⁻¹ when measured at a temperature of 120° C. and a2,2 dimethylbutane pressure of 60 torr (8 kPa). See U.S. Pat. Nos.6,423,879 and 6,504,072.

WO 99/38823 reported a reactive distillation process comprising thecontact of toluene with a methylating agent in the presence of a zeolitein a reaction/distillation column produces, as a side product, DME,which can be recycled (with unreacted methanol) to extinction in theprocess. The process operates at no greater than 320° C.

It has recently been discovered that the alkylation of benzene and/ortoluene with methanol can also result in the production of a variety ofoxygenates, in addition to DME, but also other oxygenate by-products.See for instance U.S. patent application Ser. No. 13/487,651. Accordingto the invention described in Ser. No. 13/487,651, the concentration ofphenolic impurities in a xylene stream produced by alkylation of benzeneand/or toluene with methanol can be reduced to trace levels, e.g., below0.1 ppmw, by one or more washing treatments with an aqueous solution ofa base. The resultant treated xylene stream, if necessary after waterwashing to remove any phenate-containing solution, can then be recycledto the xylene splitter to generate additional para-xylene or can be usedas a solvent. This discovery was surprising, as phenol is not present inreformate streams, which is the traditional source of xylene streams.

It has also recently been discovered that xylenes produced by alkylatingtoluene and/or benzene with an alkylating agent comprising methanoland/or DME over a solid acid catalyst contain small quantities ofstyrene, which, if not removed, could cause operability problems fordownstream paraxylene recovery processes, or even further, in processesusing paraxylene, such as the production of terephthalic acid, andderivatives thereof, including polyester fibers, films, and the like.See co-filed U.S. Patent Application PCT/US13/39184 (based on U.S.Provisional Patent Application No. 61/653,688, filed May 31, 2012, andU.S. Provisional Patent Application 61/681,486, filed Aug. 9, 2012.

Several characteristics of the xylene produced by alkylation of benzeneand/or toluene make styrene removal challenging. The desired product,paraxylene, is present at higher-than-equilibrium concentration. Thematerial used to remove phenol must therefore show minimal xylenesisomerization activity. The catalyst must also minimize formation ofbenzene, which also can have detrimental effects on downstreamprocessing. Furthermore, as discussed above, the product may alsocontain styrene as well as other olefinic compounds that may enter thealkylation reaction system via the feedstream of toluene, such ascatalytic reforming units, which are a source of toluene for theaforementioned alkylation reaction. These and other problems make thetreatment of the product stream from the alkylation of benzene and/ortoluene in the presence of an acid catalyst difficult.

It has long been known that certain substances have selective adsorptioncharacteristics useful in resolving mixtures into component parts. See,for instance, U.S. Pat. No. 4,453,029, which teaches the use of certainzeolites in selective separation of certain mono- and para-disubstitutedbenzene ring compounds and mono-substituted pyridine ring compounds inadmixture with aromatic compounds selected from the group consisting ofortho-disubstituted, meta-disubstituted and more highly substitutedbenzene ring compounds and poly-substituted pyridine ring compounds.

Other relevant prior art includes U.S. Pat. No. 6,555,611, teaching anabsorbent for aromatic hydroxyl compound comprising composite metaloxide solid solution particles or hydrotalcite-like composite metalhydroxide particles; JP 56039025A, teaching removal of phenols fromorganic matter by contact with a polyvinyl pyridine resin; CN 1253937A,teaching using silica gel to remove phenol-like compounds from styrenemonomers; U.S. Pat. No. 3,409,691, teaching removal of phenol by the useof macroporous ion exchange resin; U.S. Pat. No. 4,064,042, teachingseparating an organic component such as phenol from blood by contactwith a macroporous synthetic polymer; U.S. Pat. No. 5,218,132, teachingremoval of aromatic impurities such as phenol by contact with a materialincluding a smectite mineral; and JP 7215901A, teaching contact of aphenol-containing non-aqueous solvent with an acrylic weak basic ionexchange resin. See also U.S. Pat. Nos. 8,252,967; 7,022,161; 4,469,805;4,404,118; 2,943,105; U.S. Patent Publication 2012-0316375 and U.S.patent application Ser. No. 13/618,211.

The present inventors have surprisingly discovered a method forselective removal of phenol from a process stream comprising hydrocarbonmixtures, especially hydrocarbon mixtures that containhigher-than-equilibrium paraxylene.

SUMMARY OF THE INVENTION

The invention is directed to purification of an aromatic hydrocarbonstream including selective removal of phenol from a process stream, saidprocess comprising the contact of benzene and/or toluene with analkylating agent in the presence of a suitable alkylation catalyst underappropriate conditions to selectively produce paraxylene, said selectiveremoval of phenol comprising the contact of said process stream with asuitable material under conditions effective to provide a product streamfrom said process, said product stream having a lower concentration ofphenol than said process stream, preferably less than 10 ppm wt, morepreferably less than 1.0 ppm wt. The alkylating agent is preferablyselected from methanol, dimethylether (DME) and mixtures thereof.

The process is also directed to a process for the production ofparaxylene selectively by: (i) reacting of toluene and/or benzene withan alkylating agent, preferably methanol and/or dimethylether (DME), inthe presence of a suitable alkylation catalyst under appropriateconditions to selectively produce a process stream comprising paraxylenein higher than equilibrium amounts; and (ii) contact of said processstream comprising paraxylene in higher than equilibrium amounts with asuitable material to remove phenol and provide a product stream havinglower concentration of phenol than said process stream.

Suitable materials used to remove phenol from the process stream includealumina, silica, molecular sieves, zeolites, basic organic resins, andmixtures thereof.

In embodiments, said process stream may be subjected to additionalprocess steps such as fractionation or adsorptive separations to removespecies other than phenol. In embodiments, the process stream treated toprovide a lower concentration of phenol may be the feedstream to thealkylation process, such as the toluene stream from a catalyticreforming unit, or a stream comprising xylenes downstream of thealkylation reactor, such as upstream of a fractionator used to separateunreacted toluene (e.g., “detol fractionator”) and/or methanol from thealkylation reactor product xylene stream, the bottoms and/or overheadproduct from said detol fractionator, a xylenes splitter, such asutilized to separate heavy aromatics (C9+ aromatic hydrocarbons) fromthe xylene product, upstream or downstream from a paraxylene recoveryunit (e.g., adsorptive separation, such as a Parex™ adsorptiveseparation unit or Eluxyl™ adsorptive separation unit, or acrystallization apparatus), upstream or downstream of an isomerizationunit (which may be liquid phase or vapor phase), and the like. Theprocess stream may also comprise an imported process stream or any othertype of stream which has picked up oxygenate impurities, particularlyphenol, such as from a previous cargo.

In embodiments, the process also comprises regeneration of saidmaterial, preferably by heating under continuous flow of wet inert gas,such as at greater than or equal to 100° C. in the presence of acontinuous flow of N₂ small amounts of steam, such as amounts measuredin ppm-range (e.g., 1-1000 ppm or 10-600 ppm, or 100-500 ppm) or bycompetitive adsorption using a polar adsorbent, such as alcohols, todisplace the adsorbed phenol, and combinations thereof. In embodimentssaid regeneration may also be selected from one or more of: (1) purgewith mixture(s) of N₂ or other inert gas and at least one organicsolvent such as aromatics, alcohols, ketones, and the like or at leastone inorganic solvent such as water, CO₂, CS₂, etc., at temperaturessuch as >20° C.; (2) purge with an organic solvent such as aromatics,alcohols, ketones, etc., or an inorganic solvent such as water, CO₂,CS₂, and the like in either liquid phase or vapor phase at temperaturessuch as >20° C. followed by a N₂ (or other inert gas) purge attemperatures such as >100° C.; (3) purge with mixture(s) of at least oneorganic solvent and at least one inorganic solvent at, forinstance, >25° C., followed by a N₂ purge at temperatures such as >150°C.; and (4) purge with air, mixture of oxygen and nitrogen, steam, ormixtures thereof at, by way of example, temperatures >150° C.

By “selectively produce paraxylene” and similar phrases is meant theproduction of xylenes wherein paraxylene is present in amounts greaterthan is present in an equilibrium mixture of C8 aromatic isomers, and by“equilibrium mixture” or “equilibrium amounts” with reference to theconcentration of paraxylene in a mixture of C8 aromatic isomers is meantgenerally about 22-24 wt %. Preferably, the alkylation reaction producesa product stream having at least 70 wt %, such as 75 wt %, 80 wt %, 85wt %, 90 wt %, (all wt % herein based on the total amount of C8 aromaticisomers unless otherwise specified), to about 99 wt % or even higher,particularly in the ranges of 70-90 wt %, 75-88 wt %, 80-95 wt %, 82-88wt %, or in the range of from any lower wt % disclosed to any higher wt% disclosed.

In embodiments the amount of phenol present after said contact with acatalyst suitable for selective removal of phenol is less than 20 ppmwt, more preferably less than 10 ppm wt, still more preferably less than1 ppm wt, based on the total amount of aromatic hydrocarbon.

By “selective removal of phenol” means that the amount of phenol removedin the phenol-removal contacting step is, in embodiments, equal to orgreater than the amount of phenol produced in the alkylation reaction,or so that the final product after the styrene removal step is less than20 ppm wt, or less than 10 ppm wt, or less than 1 ppm wt., and/orgreater than the amount of benzene produced in said step, and/or greaterthan the amount of paraxylene isomerization that occurs in said phenolremoval step.

In embodiments said process stream may be subjected to additionalprocess steps such as fractionation, adsorptive separations,crystallization, membrane separation, and the like, to remove speciesother than phenol.

In embodiments, said contact may be in the presence of hydrogen or itcan be in the absence of hydrogen.

It is an object of the invention to provide a continuous,semi-continuous, or batch process of purifying xylene feedstream ofphenol and phenolic-like impurities by contact with a material, such asan adsorbent, that can be regenerated.

It is another object of the invention to provide an apparatus adaptedfor the process of the invention.

These and other objects, features, and advantages will become apparentas reference is made to the following detailed description, preferredembodiments, examples, and appended claims.

BRIEF DESCRIPTION OF THE DRAWINGS

FIGS. 1 and 2 are schematic diagrams showing certain preferredembodiments of the present invention.

FIGS. 3-4 show experimental results on one or more embodiments of theinvention.

DETAILED DESCRIPTION

According to the invention, there is a process for purification of anaromatic hydrocarbon stream by selective adsorption. By selectiveadsorption is meant that phenol is removed in amounts higher than theamount of xylenes, particularly paraxylene, such as by contact of saidstream with a material selected from alumina, silica, molecular sieves,zeolites, basic organic resins, and mixtures thereof. In a particularlypreferred embodiment it comprises removal of phenol by selectiveadsorption of phenol with a suitable adsorbent from a process streamcomprising higher than equilibrium amounts of paraxylene and alsooxygenate contaminants, wherein said higher than equilibrium amounts ofparaxylene and said oxygenate contaminants are produced by the reactionof an alkylating agent selected from methanol, DME, and mixturesthereof, with toluene and/or benzene in the presence of a suitablecatalyst under appropriate conditions.

In embodiments, the process also comprises regeneration of saidmaterial, preferably by heating under continuous flow of wet inert gas,such as at greater than or equal to 100° C. in the presence of acontinuous flow of N₂ and small amounts of steam, such as amountsmeasured in ppm-range (e.g., 1-100 ppm or 1-25 ppm, or 1-10 ppm) or bycompetitive adsorption using a polar adsorbent, such as alcohols, todisplace the adsorbed phenol, and combinations thereof. In embodimentssaid regeneration may also be selected from one or more of: (1) purgewith mixture(s) of N₂ and at least one organic solvent such asaromatics, alcohols, ketones, and the like or at least one inorganicsolvent such as water, CO₂, CS₂, etc., at temperatures such as >20° C.;(2) purge with an organic solvent such as aromatics, alcohols, ketones,etc., or an inorganic solvent such as water, CO₂, CS₂, and the like ineither liquid phase or vapor phase at temperatures such as >20° C.followed by a N₂ purge at temperatures such as >100° C.; (3) purge withmixture(s) of at least one organic solvent and at least one inorganicsolvent at, for instance, >25° C., followed by a N₂ purge attemperatures such as >150° C.; and (4) purge with air, mixture of oxygenand nitrogen, low amount of steam (again, at ppm levels), or mixturethereof at, by way of example, temperatures >150° C.

Successful regeneration in the presence of low levels of steam issurprising as heretofore it would be thought that such materials wouldconvert essentially to a cement-like material when contacted with steam.

In embodiments the preferred adsorbents are selected from alumina,silica, molecular sieves and/or zeolites, basic organic resins, andmixtures thereof, and in still a more preferred embodiment areAmberlyst™ A26OH and/or Selexorb™ CDX. There terms “molecular sieve” and“zeolites” are used synonymously herein.

In preferred embodiments, there is also a step of recovery of paraxyleneby crystallization, adsorption, and the like. More preferably, after theselective adsorption of phenol with a suitable adsorbent, to provide aphenol-depleted stream comprising xylenes, there is the step ofselective removal of paraxylene to provide a paraxylene-enrichedaromatic hydrocarbon stream and a paraxylene-depleted aromatichydrocarbon stream. Particularly preferred methods include use of aParex™ unit or Eluxyl™ unit.

A typical composition of xylenes produced from the reaction of toluenewith methanol in the presence of a solid acid catalyst is shown in Table1.

TABLE 1 Compound wt % Toluene 0.0950 Styrene 0.0648 mixed xylenes 94.56Ethylbenzene 0.47 C9 aromatics 4.7574 Phenol 0.0014 other oxygenates>0.05

Representative species found in the product include1,2,4-trimethylbenzene, 1-methyl-4-ethylbenzene, n-nonane, naphthalene,1,4-dimethyl-2-ethylbenzene, biphenyl, anthracene, C16 aromaticalkylates, benzoic acid, 4-methylbenzoic acid, o-cresol,2,4-dimethylphenol, and the like.

The presence of phenol and phenolic species in a stream of xylenes inprocesses downstream of their production, e.g., the preparation ofterephthalic acid and derivatives thereof, can be a problem, anddepending on the final product, need to be present in very small tovanishing (no trace) amounts.

The invention may still better be understood by reference to thefollowing specific examples, which are intended to illustrate, but notlimit, the scope of this invention. One of skill in the art inpossession of the present disclosure will appreciate that the inventionmay be practiced other than as specifically illustrated.

Examples 1-14 Phenol Adsorption with Selexorb™ CDX at 40° C. and 20° C.

Pre-weighted and pre-dried adsorbent Selexorb CDX was added to mixedxylene solutions that contained phenol of various concentrations. Themixtures were kept at 40° C. or 20° C. for 96 hours. Phenolconcentration of the hydrocarbon solution was then determined by GCchromatography. Results, shown in Table 1, demonstrated Selexorb CDX'scapability in selective adsorption of phenol in hydrocarbons.

Examples 15-20 Regeneration of Selexorb™ CDX Adsorbent

Pre-weighted and pre-dried adsorbent Selexorb CDX (˜2.30 grams) wasadded to mixed xylene solutions (˜8.70 grams) that contained phenol ofvarious concentrations. The mixture was kept at 40° C. for 96 hours.Afterwards, the spent adsorbents were recovered by filtration andregenerated under a continuous N₂ flow at temperatures of 150, 200, and280° C. for 72 hours, respectively. The regenerated adsorbents were thenused in the second cycle of phenol adsorption experiment. Thisadsorption-regeneration cycle was repeated.

Table 2 lists phenol concentrations in hydrocarbons after eachadsorption cycle. A comparison of this data from these consecutivecycles suggested that regeneration under a continuous purge of inert gassuch as N₂ recovered the majority of Selexorb CDX's phenol adsorptioncapacity.

Example 21 Phenol Adsorption with Selexorb™ CDX in Presence of Styrene

The above experiment was repeated with Selexorb CDX with a hydrocarbonsolution that contained phenol and styrene. Results, shown in Table 3,demonstrated Selexorb CDX's selectivity towards phenol when ahydrocarbon solution contains both styrene and phenol.

Example 22 Phenol Adsorption with Selexorb™ CDX in Presence ofStyrene—Regeneration

The spent absorbent from Experiment 21 was recovered and regeneratedunder a continuous N₂ flow at 280° C. for 72 hours. The regeneratedadsorbent was then used in the 2^(nd) cycle of the phenol adsorptionexperiment. Results, shown in Table 3, indicated that Selexorb CDXretained its selectivity towards phenol after the regeneration.

Examples 23-26 Phenol Adsorption with Amberlyst™ A26OH at 20° C. and 40°C.

Experiments 1-14 were repeated with Amberlyst A26OH as the adsorbent at20° C. and 40° C., respectively. Results, shown in Table 4, indicatedAmberlyst A26OH's ability to selectively adsorb phenol in hydrocarbons.

TABLE 1 Adsorption of Phenol in Hydrocarbon with Selexorb ™ CDXHydrocarbon Solutions Phenol Concentration, ppm Temperature, AdsorbentBefore After Experiment ° C. Name Weight (g) Weight (g) AdsorptionAdsorption 1 40 Selexorb CDX 2.31 8.71 1,122 0.42 2 40 Selexorb CDX 2.318.71 2,129 1.65 3 40 Selexorb CDX 2.34 8.72 3,168 1.84 4 40 Selexorb CDX2.30 8.75 4,149 2.67 5 40 Selexorb CDX 2.30 8.72 6,124 5.44 6 40Selexorb CDX 2.29 8.68 8,010 11.43 7 40 Selexorb CDX 2.33 8.75 11,19142.91 8 20 Selexorb CDX 2.33 8.71 1,122 0.00 9 20 Selexorb CDX 2.30 8.754,149 1.52 10 20 Selexorb CDX 2.32 8.70 10,258 4.38 11 20 Selexorb CDX2.26 8.56 11,191 7.73 12 20 Selexorb CDX 2.30 8.71 14,380 15.33 13 20Selexorb CDX 2.31 8.70 17,549 39.85 14 40 Selexorb CDX 2.50 8.71 2,1667.04

TABLE 2 Adsorption of Phenol in Hydrocarbon with Selexorb - AdsorbentRegeneration Experiment 15 16 17 18 19 20 Regen Temp (° C.) 150 150 200200 280 280 Initial Phenol Conc (wt %) 0.2 0.4 0.2 0.4 0.2 0.4Adsorption Cycle Phenol Concentration after Adsorption (ppm) 1 4.35 6.3511.43 5.44 2.67 4.29 2 17.80 52.25 511.77 250.77 37.84 25.48 3 8.0422.15 19.49 27.57 1.29 6.51 4 3.12 23.39 1.73 18.63 0.35 4.73 5 17.8083.00 4.30 12.40 1.50 6.70 6 24.80 69.36 10.13 41.93 4.51 17.90 7 155.87565.45 79.99 223.65 26.43 134.11 8 156.19 645.16 316.80 32.12 6.23 23.769 767.24 1830.25 113.12 291.22 31.72 233.53 10 370.98 1128.19 35.10134.06 17.62 82.21 11 595.98 1324.23 71.42 181.17 28.78 122.40 12 57.8826.10 123.70 13 59.59 32.64 103.03 14 86.85 72.30 170.87

TABLE 3 Adsorption of Phenol in Styrene-containing Hydrocarbons withSelexorb ™ CDX Experiment 21 22 Adsorption Cycle Fresh 2 Regen Temp (degC.) 280 Initial Phenol Conc (wt %) 0.22 0.22 Final Phenol Concentration,ppm 4.12 7.04 Initial Styrene Conc (ppm) 19.50 19.53 Final Styrene Conc(ppm) 19.70 19.32

TABLE 4 Adsorption of Phenol in Hydrocarbons with Amberlyst ™ A26OHHydrocarbon Solutions Adsorbent Phenol Concentration, ppm Temperature,Weight Weight Before After Experiment ° C. Name (g) (g) AdsorptionAdsorption 23 40 Amberlyst A26OH 2.32 8.70 1,984 96 24 40 AmberlystA26OH 2.30 8.73 3,926 148 25 40 Amberlyst A26OH 2.30 8.66 6,135 815 2640 Amberlyst A26OH 2.30 8.71 8,242 898 27 40 Amberlyst A26OH 2.31 8.7110,258 1,150 28 20 Amberlyst A26OH 2.30 8.72 1,984 65 29 20 AmberlystA26OH 2.31 8.76 3,926 197 30 20 Amberlyst A26OH 2.33 8.76 6,124 366 3120 Amberlyst A26OH 2.31 8.69 8,010 737 32 20 Amberlyst A26OH 2.30 8.7110,258 801

The following additional experiments are also intended to berepresentative and not limiting.

Example 27 Adsorption on Fresh Selexsorb CDX at 5 WHSV

A fixed bed of fresh Selexsorb CDX alumina obtained from the BASFCompany was mixed with quartz sand in a ⅜″ stainless reactor. Themixture was dried at 280° C. under continuous N₂ flow for 14-20 hrs.Afterwards, a mixed xylene solution containing 6.5 ppm phenol was fedinto the reactor at 40° C. and 5 WHSV. Samples of outlet liquids werecollected at regular intervals and analyzed for the phenolconcentration. Results are plotted in FIG. 3.

Example 28 Adsorption on the 1st Cycle N2-Regenerated Selexsorb CDX at 5WHSV

The spent adsorbent from Example 27 was regenerated at 280° C. undercontinuous N2 flow. After regeneration, the adsorbent was tested forphenol adsorption, following the same procedure as that of Example 27.Results are shown in FIG. 3.

Example 29 Adsorption on the 7th Cycle N2-Regenerated Selexsorb CDX at 5WHSV

A spent adsorbent Selexsorb CDX, regenerated with N2 at 80° C. for seventimes, was used in phenol adsorption, following the same procedure asthat of Example 27. Results are shown in FIG. 3.

Example 30 Adsorption on Fresh Selexsorb CDX at 20 WHSV

A fixed bed of fresh Selexsorb CDX and quartz sand in a ⅜″ stainlessreactor was dried at 280° C. under a continuous N2 flow for 14-20 hrs.Afterwards, a mixed xylene solution containing 6.7 ppm phenol was fedinto the reactor at 40° C. and 20 WHSV. Samples of outlet liquids werecollected at regular intervals and analyzed for the phenolconcentration. Results are plotted in FIG. 4.

Example 31 Adsorption on the 1st Cycle Wet-Toluene-Regenerated SelexsorbCDX at 20 WHSV

The spent adsorbent from Example 30 was regenerated with wet toluene attemperature 120° C. at 5 WHSV. The wet toluene contained ˜400 ppm H2Ounder a continuous N2 flow. Samples of outlet liquids were collected atregular intervals and analyzed for the phenol concentration. The last 46hours of the regeneration was at 150° C.

After the wet toluene regeneration, the spent adsorbent was dried at150° C., then 220° C., and 280° C. for 24 hours, respectively. The driedadsorbent was then used in phenol adsorption, following the sameprocedure as that of Example 30. Results are shown in FIG. 4.

Example 32 Adsorption on the 2nd Cycle Wet-Toluene-Regenerated SelexsorbCDX at 20 WHSV

The spent adsorbent from Example 31 was regenerated the second time withwet toluene at temperature 150° C. at 5 WHSV, following the sameprocedure as that of Example 5. The last 46 hours of the regenerationwas at 200° C. The regenerated spent adsorbent, after drying at 150° C.,then 220° C., and 280° C. for 24 hours, respectively, was used in phenoladsorption, also following the same procedure as that of Example 30.Results are shown in FIG. 4.

The alkylation process employed herein can employ any aromatic feedstockcomprising toluene and/or benzene, although in general, it is preferredthat the aromatic feed contains at least 90 wt %, especially at least 99wt % of benzene, toluene or a mixture thereof. An aromatic feedcontaining at least 99 wt % toluene is particularly desirable.Similarly, although the composition of the methanol- and/ordimethylether-containing feed is not critical, it is generally desirableto employ feeds containing at least 90 wt %, especially at least 99 wt%, of methanol and/or dimethylether. Water is also advantageously usedin the feed to the alkylation reaction.

In embodiments said process stream may be subjected to additionalprocess steps such as fractionation, adsorptive separations,crystallization, membrane separation, and the like, to remove speciesother than phenol.

The invention may yet still be even better understood by reference toFIGS. 1 and 2, which are schematic illustrations of preferredembodiments of the invention. One of skill in the art in possession ofthe present discourse will understand that the invention may bepracticed other than as specifically illustrated herein, and theillustrations is not intended to be limiting.

In FIG. 1, apparatus 1 is a reactor suitable for carrying out alkylationof benzene and/or toluene in the presence of a solid acid catalyst, suchas ZSM-5, particularly a phosphorus-containing ZSM-5, and moreparticularly a phosphorus-containing ZSM-5 that has been steamed attemperatures on the order of 1000° F. The specifics of the apparatus 1do not form a part of the present invention, except as otherwise statedherein, but rather have been described in numerous prior art patents,patent applications, and publications.

The effluent from 1, which is an aromatic hydrocarbon stream rich inparaxylene, such as 70 wt % or more, as described in more detail herein,is passed via conduit 11 to phenol removal unit 2A. The unit 2A isillustrated with dotted lines since it is but one possible placement ofsuch a unit, albeit preferred, according to embodiments of theinvention. The phenol-depleted stream rich in paraxylene is passed viaconduit 12 to a fractionation column or splitter 3 wherein the stream issplit into a paraxylene-enriched overhead passed downstream in theprocess through conduit 13 and a paraxylene depleted bottoms productpassed downstream in the process through conduit 14.

Phenol removal unit 2B illustrates a second possible placement of aphenol removal unit according to the present invention. One or both of2A and 2B may be used in an embodiment of the process according to theinvention. Phenol removal units may comprise one or more vesselscontaining, by way of example, a fixed bed apparatus comprising theadsorbent. Such units are per se known in the art.

The paraxylene-enriched overhead from splitter 3, is passed via conduit15 to an optional second fractionation column 7, or in the case whereunit 2A is not present, a first phenol removal unit 2B. Theparaxylene-enriched stream 15, now having been treated by one or both ofphenol removal units 2A and/or 2B is then passed via conduit 15 tofractionator 7 to remove heavies such as aromatic C9+s 21 and pass anoverhead 16, comprising an paraxylene-enriched, phenol-depleted stream(relative to effluent 11), further downstream in the process. Thisstream 16 may optionally be treated in apparatus 4 to remove otherimpurities, such as other oxygenates, e.g., by caustic wash (see U.S.patent application Ser. No. 13/487,651) or styrene, as explained in U.S.Provisional Patent Application No. 61/653,688. The stream 17 is thensent to paraxylene removal unit 5 of the type known in the art, such asan adsorptive separation unit (e.g., Parex™ unit or Eluxyl™ unit) orseparation by crystallization. The final desired high purity paraxylenestream is taken off via conduit 18 and the paraxylene-depleted stream22, otherwise known as raffinate with respect to paraxylene removalunits, is sent to a liquid phase isomerization unit 6, of the type perse well-known in the art, wherein the paraxylene-depleted raffinate isisomerized to equilibrium concentration xylenes (i.e., about 22-24 wt %paraxylene). The isomerization may be liquid phase or vapor phase, eachper se known in the art. After isomerization the equilibrium xylenesstream may be recycled via line 20 to fractionator 7 or otherwiseprocessed as desired.

The invention may be still be even better understood by reference toFIG. 2, which is a schematic illustration of another preferredembodiment of the invention. FIG. 2 illustrates apparatus downstream ofthe alkylation reactor, not shown for convenience of view. In FIG. 2,fresh feed 100, comprising alkylating agents selected from methanol,DME, or a combination thereof, and/or the aromatic species to bealkylated, selected from benzene, toluene, and mixtures thereof, arepassed through phenol-removal unit 101 and then via conduit 102 tostyrene-removal unit 103, and then through conduit 104 to fractionator110, which removes toluene overhead to be sent to the alkylationreactor, as described further hereinbelow. One of the advantages of thepresent invention is that one or more of extracted toluene andnon-extracted toluene may be used, and since numerous sources of toluenecan be used in the alkylation reactor using a solid acid catalyst, aswell as numerous sources of methanol and/or DME alkylating agent. Thus,it is advantageous to have a pre-treatment of the feed(s) in one or bothof units 101 and 103 as set forth in FIG. 2, however, use of suchpretreatment is optional. It will also be appreciated that thealkylating agent(s) and benzene and/or toluene can be fed separatelytogether, and likewise the choice of whether to have a pretreatment byone or both of units 101 and 103, in either order, can be madeindependently on each separate feedstream. Water is advantageously alsoadded to the upstream alkylation reactor and may be added into thesystem represented by the entirety of the alkylation reactor (not shown)and the apparatus shown in FIG. 2 along with feed 100, or it may beadded separately to said system directly to the alkylation reactor; theaddition of water and the location of addition is optional.Advantageously, the addition of water into the alkylation reactor is inan amount sufficient to reduce coking of the catalyst. One or more ofthe feeds may be added preheated and the feed(s) may be added as liquidor vapor to reactor 100.

Continuing with FIG. 2, 105 represents one or more of the recycledreactor products, advantageously previously treated to remove gaseousproducts (e.g., light olefins) and possibly dried of water, although, asmentioned above, water may be added as part of the feed. The removal ofgaseous products and/or water is not shown in FIG. 2 as it does not forma part of the present invention per se, and could be accomplished by oneof ordinary skill in the art in possession of the present disclosure.Typically unreacted methanol and/or DME and unreacted benzene and/ortoluene are recycled via line 105 or they may be recycled separately, ora combination thereof, and thus pretreatment by phenol-removal unit 106and/or styrene removal unit 108, fluidly connected to 106 via line 107and to reactor 110 via line 109, is advantageous.

Continuing with FIG. 2, fractionator tower 110 (or “detol tower”)removes toluene overhead and the toluene can optionally be sent viaconduit 111 through one or more of phenol removal unit 112 and styreneremoval unit 114, fluidly connected by conduit 113, prior to beingrecycled to the alkylation reactor (again, not shown) via conduit 115.It will be appreciated that the toluene stream 111 may be optionallycooled to a liquid by known methods, not shown, prior to treatment inunits 112 and/or 114, and that whether or not to have a phenol removalstep and/or styrene removal step between the detol tower 110 and thealkylation reactor, and the order thereof, can be determinedindependently by one of ordinary skill in the art in possession of thepresent disclosure.

The bottoms product of detol tower 110, comprising the desiredparaxylene-enriched alkylation reactor products, leaves 110 throughconduit 116 and may optionally be treated by one or more of the phenolremoval unit 117 and/or the styrene removal unit 119, fluidly connectedby conduit 118, and is then passed to xylene splitter 121 via conduit120 to remove heavier products (i.e., C9+ aromatic hydrocarbons) as abottoms product through conduit 122. The C9+s may be advantageous usedwith a transalkylation unit integrated with the system shown in FIG. 2,and indeed the entire apparatus shown in FIG. 2, and the alkylationreactor not shown, may be advantageous integrated with other knownmethods of generating xylenes and/or other aromatic products, forgreater efficiency of feedstream use, integration of heat (which inembodiments is generated by the alkylation reactor), and so on.

The overheads 123 from xylene splitter 121 may also optionally betreated by one or both of phenol removal unit 124 and styrene removalunit 126, fluidly connected via conduit 125 prior to being sent viaconduit 127 to an optional second xylene splitter 128, which analogousto splitter 121, separates the desired paraxylene-enriched xylenesstream overhead, to conduit 130, from bottoms product 129, which mayagain be disposed of in the same manner as bottoms product 122.

The overheads 130 may be treated by one or both of a phenol removal unitor styrene removal unit, and in the embodiment of FIG. 2, is illustratedby a single unit 131, which may represent one or more of such units.

The remaining portions of FIG. 2 are similar to the per se well-knownxylenes loop, but integrated with the phenol removal step(s) accordingto the present invention, and thus, the paraxylene-enriched stream 132is passed to a paraxylene recovery unit 133, which may be an adsorptionunit (e.g., Parex adsorption unit or Eluxyl adsorption unit), or acrystallizer unit, or membrane unit, and the like, wherein paraxylene isseparated from its C8 aromatic isomers, to yield very high purityparaxylene via conduit 134, which may yet further be treated by one ormore of a phenol-removal unit and/or styrene removal unit, representedby a single apparatus 135, to yield a highly pure, highly enrichedparaxylene product, having, in embodiments, a paraxylene content ofgreater than 99.0 wt % (based on the entire content of the stream), andfurther characterized by a phenol content of less than 10 ppm wt,preferably less than 1.0 ppm wt.

Finally, continuing with the description of the embodiment shown in FIG.2, the raffinate (paraxylene-depleted xylenes stream) from theparaxylene removal unit 133, leaving via conduit 137, may be recoveredas mixed xylenes 139, optionally but advantageously treated by one ormore of a styrene removal unit and/or a phenol removal unit, againrepresented by a single apparatus 138, and/or via conduit 140 to theisomerization unit represented by apparatus 143, optionally butadvantageously treated by one or more of a styrene removal unit and/or aphenol removal unit, again represented by a single apparatus 141 whichis fluidly connected to isomerization unit 143 by conduit 142. Theproduct of the isomerization unit, as is well-known, will be anequilibrium stream of xylenes, which may be advantageously then recycledback xylenes splitter 128 and/or sent to ethylbenzene purge (not shown)via conduit 145, optionally treated by one or more of phenol removaland/or styrene removal unit, again represented by a single unit 146,leaving said unit, if present, via conduit 147.

The isomerization unit 143 may be liquid phase or gas phase or both maybe used in series or parallel. Both liquid and gas phase isomerizationprocesses and units to use in said processes are per se well-known inthe art.

The catalyst employed in the alkylation process is generally a porouscrystalline material and, in one preferred embodiment, is a porouscrystalline material having a Diffusion Parameter for 2,2 dimethylbutaneof about 0.1-15 sec⁻¹ when measured at a temperature of 120° C. and a2,2 dimethylbutane pressure of 60 torr (8 kPa).

As used herein, the Diffusion Parameter of a particular porouscrystalline material is defined as D/r²×10⁶, wherein D is the diffusioncoefficient (cm²/sec) and r is the crystal radius (cm). The diffusionparameter can be derived from sorption measurements provided theassumption is made that the plane sheet model describes the diffusionprocess. Thus, for a given sorbate loading Q, the value Q/Q_(eq), whereQ_(eq) is the equilibrium sorbate loading, is mathematically related to(Dt/r²)^(1/2) where t is the time (sec) required to reach the sorbateloading Q. Graphical solutions for the plane sheet model are given by J.Crank in “The Mathematics of Diffusion”, Oxford University Press, ElyHouse, London, 1967.

The porous crystalline material is preferably a medium-pore sizealuminosilicate zeolite. Medium pore zeolites are generally defined asthose having a pore size of about 5 to about 7 Angstroms, such that thezeolite freely sorbs molecules such as n-hexane, 3-methylpentane,benzene and p-xylene. Another common definition for medium pore zeolitesinvolves the Constraint Index test which is described in U.S. Pat. No.4,016,218, which is incorporated herein by reference. In this case,medium pore zeolites have a Constraint Index of about 1-12, as measuredon the zeolite alone without the introduction of oxide modifiers andprior to any steaming to adjust the diffusivity of the catalyst. Inaddition to the medium-pore size aluminosilicate zeolites, other mediumpore acidic metallosilicates, such as silicoaluminophosphates (SAPOs),can be used in the present process.

Particular examples of suitable medium pore zeolites include ZSM-5,ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35, and ZSM-48, with ZSM-5 andZSM-11 being particularly preferred. In one embodiment, the zeoliteemployed in the process of the invention is ZSM-5 having a silica toalumina molar ratio of at least 250, as measured prior to any treatmentof the zeolite to adjust its diffusivity.

Zeolite ZSM-5 and the conventional preparation thereof are described inU.S. Pat. No. 3,702,886. Zeolite ZSM-11 and the conventional preparationthereof are described in U.S. Pat. No. 3,709,979. Zeolite ZSM-12 and theconventional preparation thereof are described in U.S. Pat. No.3,832,449. Zeolite ZSM-23 and the conventional preparation thereof aredescribed in U.S. Pat. No. 4,076,842. Zeolite ZSM-35 and theconventional preparation thereof are described in U.S. Pat. No.4,016,245. ZSM-48 and the conventional preparation thereof is taught byU.S. Pat. No. 4,375,573. The entire disclosures of these U.S. patentsare incorporated herein by reference.

The medium pore zeolites described above are preferred for the presentprocess since the size and shape of their pores favor the production ofp-xylene over the other xylene isomers. However, conventional forms ofthese zeolites have Diffusion Parameter values in excess of the 0.1-15sec⁻¹ range desired for the present process. Nevertheless, the requireddiffusivity can be achieved by severely steaming the zeolite so as toeffect a controlled reduction in the micropore volume of the catalyst tonot less than 50%, and preferably 50-90%, of that of the unsteamedcatalyst. Reduction in micropore volume is monitored by measuring then-hexane adsorption capacity of the zeolite, before and after steaming,at 90° C. and 75 torr n-hexane pressure.

Steaming to achieve the desired reduction in the micropore volume of theporous crystalline material can be effected by heating the material inthe presence of steam at a temperature of at least about 950° C.,preferably about 950 to about 1075° C., and most preferably about 1000to about 1050° C. for about 10 minutes to about 10 hours, preferablyfrom 30 minutes to 5 hours.

To effect the desired controlled reduction in diffusivity and microporevolume, it may be desirable to combine the porous crystalline material,prior to steaming, with at least one oxide modifier, preferably selectedfrom oxides of the elements of Groups IIA, IIIA, IIIB, IVA, VA, VB andVIA of the Periodic Table (IUPAC version). Conveniently, said at leastone oxide modifier is selected from oxides of boron, magnesium, calcium,lanthanum and preferably phosphorus. In some cases, it may be desirableto combine the porous crystalline material with more than one oxidemodifier, for example a combination of phosphorus with calcium and/ormagnesium, since in this way it may be possible to reduce the steamingseverity needed to achieve a target diffusivity value. The total amountof oxide modifier present in the catalyst, as measured on an elementalbasis, may be between about 0.05 and about 20 wt %, such as betweenabout 0.1 and about 10 wt %, based on the weight of the final catalyst.

Where the modifier includes phosphorus, incorporation of the modifier inthe alkylation catalyst is conveniently achieved by the methodsdescribed in U.S. Pat. Nos. 4,356,338; 5,110,776; 5,231,064; and5,348,643; the entire disclosures of which are incorporated herein byreference. Treatment with phosphorus-containing compounds can readily beaccomplished by contacting the porous crystalline material, either aloneor in combination with a binder or matrix material, with a solution ofan appropriate phosphorus compound, followed by drying and calcining toconvert the phosphorus to its oxide form. Contact with thephosphorus-containing compound is generally conducted at a temperatureof about 25° C. and about 125° C. for a time between about 15 minutesand about 20 hours. The concentration of the phosphorus in the contactmixture may be between about 0.01 and about 30 wt %.

Representative phosphorus-containing compounds which may be used toincorporate a phosphorus oxide modifier into the catalyst of theinvention are set forth in U.S. Pat. No. 6,504,072.

Particular phosphorus-containing compounds include ammonium phosphate,ammonium dihydrogen phosphate, diammonium hydrogen phosphate, diphenylphosphine chloride, trimethylphosphite, phosphorus trichloride,phosphoric acid, phenyl phosphine oxychloride, trimethylphosphate,diphenyl phosphinous acid, diphenyl phosphinic acid,diethylchlorothiophosphate, methyl acid phosphate, and otheralcohol-P₂O₅ reaction products.

Representative boron-containing compounds which may be used toincorporate a boron oxide modifier into the catalyst of the inventioninclude boric acid, trimethylborate, boron oxide, boron sulfide, boronhydride, butylboron dimethoxide, butylboric acid, dimethylboricanhydride, hexamethylborazine, phenyl boric acid, triethylborane,diborane and triphenyl boron.

Representative magnesium-containing compounds include magnesium acetate,magnesium nitrate, magnesium benzoate, magnesium propionate, magnesium2-ethylhexoate, magnesium carbonate, magnesium formate, magnesiumoxylate, magnesium bromide, magnesium hydride, magnesium lactate,magnesium laurate, magnesium oleate, magnesium palmitate, magnesiumsalicylate, magnesium stearate and magnesium sulfide.

Representative calcium-containing compounds include calcium acetate,calcium acetylacetonate, calcium carbonate, calcium chloride, calciummethoxide, calcium naphthenate, calcium nitrate, calcium phosphate,calcium stearate and calcium sulfate.

Representative lanthanum-containing compounds include lanthanum acetate,lanthanum acetylacetonate, lanthanum carbonate, lanthanum chloride,lanthanum hydroxide, lanthanum nitrate, lanthanum phosphate andlanthanum sulfate.

The porous crystalline material employed in the process of the inventionmay be combined with a variety of binder or matrix materials resistantto the temperatures and other conditions employed in the process. Suchmaterials include active and inactive materials such as clays, silicaand/or metal oxides such as alumina. The latter may be either naturallyoccurring or in the form of gelatinous precipitates or gels includingmixtures of silica and metal oxides. Use of a material which is active,tends to change the conversion and/or selectivity of the catalyst andhence is generally not preferred. Inactive materials suitably serve asdiluents to control the amount of conversion in a given process so thatproducts can be obtained economically and orderly without employingother means for controlling the rate of reaction. These materials may beincorporated into naturally occurring clays, e.g., bentonite and kaolin,to improve the crush strength of the catalyst under commercial operatingconditions. Said materials, i.e., clays, oxides, etc., function asbinders for the catalyst. It is desirable to provide a catalyst havinggood crush strength because in commercial use it is desirable to preventthe catalyst from breaking down into powder-like materials. These clayand/or oxide binders have been employed normally only for the purpose ofimproving the crush strength of the catalyst.

Naturally occurring clays, which can be composited with the porouscrystalline material, include the montmorillonite and kaolin family,which families include the subbentonites, and the kaolins commonly knownas Dixie, McNamee, Georgia and Florida clays or others in which the mainmineral constituent is halloysite, kaolinite, dickite, nacrite, oranauxite. Such clays can be used in the raw state as originally mined orinitially subjected to calcination, acid treatment or chemicalmodification.

In addition to the foregoing materials, the porous crystalline materialcan be composited with a porous matrix material such as silica-alumina,silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia,silica-titania as well as ternary compositions such assilica-alumina-thoria, silica-alumina-zirconia silica-alumina-magnesiaand silica-magnesia-zirconia.

The relative proportions of porous crystalline material and inorganicoxide matrix vary widely, with the content of the former ranging fromabout 1 to about 90% by weight and more usually, particularly when thecomposite is prepared in the form of beads, in the range of about 2 toabout 80 wt % of the composite.

The alkylation process can be conducted in any known reaction vessel butgenerally the methanol and aromatic feeds are contacted with thecatalyst described above with the catalyst particles being disposed inone or more fluidized beds. Each of the methanol and aromatic feeds canbe injected into the fluidized catalyst in a single stage. However, inone embodiment, the methanol feed is injected in stages into thefluidized catalyst at one or more locations downstream from the locationof the injection of the aromatic reactant into the fluidized catalyst.For example, the aromatic feed can be injected into a lower portion of asingle vertical fluidized bed of catalyst, with the methanol beinginjected into the bed at a plurality of vertically spaced intermediateportions of the bed and the product being removed from the top of thebed. Alternatively, the catalyst can be disposed in a plurality ofvertically spaced catalyst beds, with the aromatic feed being injectedinto a lower portion of the first fluidized bed and part of the methanolbeing injected into an intermediate portion of the first bed and part ofthe methanol being injected into or between adjacent downstream catalystbeds.

The conditions employed in the alkylation stage of the present processare not narrowly constrained but, in the case of the methylation oftoluene, generally include the following ranges: (a) temperature betweenabout 500 and about 700° C., such as between about 500 and about 600°C.; (b) pressure of between about 1 atmosphere and about 1000 psig(between about 100 and about 7000 kPa), such as between about 10 psigand about 200 psig (between about 170 and about 1480 kPa); (c) molestoluene/moles methanol (in the reactor charge) of at least about 0.2,such as from about 0.2 to about 20; and (d) a weight hourly spacevelocity (“WHSV”) for total hydrocarbon feed to the reactor(s) of about0.2 to about 1000, such as about 0.5 to about 500 for the aromaticreactant, and about 0.01 to about 100 for the combined methanol reagentstage flows, based on total catalyst in the reactor(s).

The product of the reaction between the methanol and the aromatic feedis a gaseous effluent comprising para-xylene and other xylene isomers,water vapor, unreacted toluene and/or benzene, unreacted methanol,phenolic impurities, light olefins and other light gas by-products, andgenerally some C₉+ aromatic by-products. In addition, where the processis conducted in a fluidized catalyst bed, the effluent will contain someentrained solid catalyst and catalyst fines. Thus, the gaseous effluentleaving the (final) fluidized bed reactor is generally passed through anintegral cyclone separator to remove some of the entrained catalystsolids and return them to the alkylation reactor.

The product effluent leaves the alkylation reactor system at a hightemperature, typically between about 500 and about 600° C. and initiallymay be passed through a heat exchanger so that the waste heat in theeffluent stream may be recovered and used to heat other processstream(s). It is, however, preferred that any initial cooling of theproduct stream is limited so as to keep the effluent vapors well abovethe dew point, typically about 240° F. (116° C.).

Following further cooling, the effluent vapor stream is fed to aseparation system, which may comprise one or more fractionation columns,where the unreacted methanol and aromatics are recovered and recycled tothe alkylation step, the light and heavy hydrocarbons are removed andthe remainder of effluent is separated into a liquid organic phase richin xylene and a waste water stream. Part of the phenolic impurities isconcentrated in the xylene-rich organic phase and part is dissolved inthe waste water stream making the waste water stream acidic.

Typically, the phenolic impurities include phenol, methyl phenols anddimethyl phenols and are present in the xylene filtrate in an amountfrom about 0.2 ppmw to about 1000 ppmw of phenol, from about 0.2 ppmw toabout 1000 ppmw of methyl phenols and from about 0.5 ppmw to about 1000ppmw of dimethyl phenols.

The present invention can be integrated with other systems using tolueneand benzene streams, such as selective disproportionation of tolueneand/or transalkylation of toluene and aromatic C9+ species.

The invention has been described above with reference to numerousembodiments and specific examples. Many variations will suggestthemselves to those skilled in this art in light of the above detaileddescription.

Trade names used herein are indicated by a ™ symbol or ® symbol,indicating that the names may be protected by certain trademark rights,e.g., they may be registered trademarks in various jurisdictions. Allpatents and patent applications, test procedures (such as ASTM methods,UL methods, and the like), and other documents cited herein are fullyincorporated by reference to the extent such disclosure is notinconsistent with this invention and for all jurisdictions in which suchincorporation is permitted. When numerical lower limits and numericalupper limits are listed herein, ranges from any lower limit to any upperlimit are contemplated. While the illustrative embodiments of theinvention have been described with particularity, it will be understoodthat various other modifications will be apparent to and can be readilymade by those skilled in the art without departing from the spirit andscope of the invention. Accordingly, it is not intended that the scopeof the claims appended hereto be limited to the examples anddescriptions set forth herein but rather that the claims be construed asencompassing all the features of patentable novelty which reside in thepresent invention, including all features which would be treated asequivalents thereof by those skilled in the art to which the inventionpertains.

What is claimed is:
 1. An apparatus comprising an alkylation reactor forthe reaction of toluene and/or benzene with an alkylating agent selectedfrom methanol, dimethylether (DME), and mixtures thereof, in thepresence of a suitable catalyst under appropriate conditions to producean aromatic hydrocarbon stream comprising paraxylene and phenolicimpurities fluidly connected with at least one phenol removal apparatusadapted for the removal of phenolic impurities by contacting saidaromatic hydrocarbon stream with an adsorbent selective for the removalof phenolic impurities from said aromatic hydrocarbon stream, whereinthe amount of phenolic impurities removed from said aromatic hydrocarbonstream is greater than the amount of benzene produced or paraxyleneisomerized by said contact, and wherein said adsorbent is selected fromalumina, silica, molecular sieves, basic organic resins, and mixturesthereof.
 2. The apparatus according to claim 1, further comprising anapparatus adapted for styrene removal, wherein said styrene removalapparatus contains a material selective for the removal of styrenerelative to the removal of phenol, and wherein said adsorbent isselective for the removal of phenol relative to styrene.
 3. Theapparatus according to claim 1, further comprising a fractionation towerfluidly connected to said alkylation reactor and said phenol removalapparatus to separate the aromatic hydrocarbon stream into a C⁸⁻hydrocarbon stream and a C₉₊ hydrocarbon stream.
 4. The apparatusaccording to claim 3, further comprising a paraxylene recovery unitfluidly connected with said alkylation reactor and said phenol removalapparatus to produce a paraxylene-enriched stream and aparaxylene-depleted stream from said C⁸⁻ hydrocarbon stream.
 5. Theapparatus according to claim 4, further comprising a liquidisomerization unit fluidly connected to said paraxylene recovery unit toisomerize the paraxylene-depleted stream.
 6. The apparatus according toclaim 4, further comprising a liquid isomerization unit fluidlyconnected to said paraxylene recovery unit and a vapor isomerizationunit fluidly connected to said paraxylene recovery unit, wherein saidliquid isomerization unit and said vapor isomerization unit are operatedin series or parallel, to isomerize the paraxylene-depleted stream andproduce equilibrium xylenes.
 7. The apparatus according to claim 3,wherein said fractionation tower is downstream of said alkylationreactor and upstream of said paraxylene removal unit, and furtherwherein said phenol removal apparatus is downstream of said alkylationreactor and upstream of said fractionation tower.
 8. The apparatusaccording to claim 4, wherein said phenol removal apparatus isdownstream of said alkylation reactor and upstream of said paraxylenerecovery system.
 9. The apparatus according to claim 4, wherein saidfractionation tower is downstream of said alkylation reactor andupstream of said paraxylene removal unit, and further wherein saidphenol removal apparatus is downstream of said fractionation tower andupstream of said paraxylene removal unit.
 10. The apparatus according toclaim 5, wherein said phenol removal apparatus is downstream of saidparaxylene recovery unit and upstream of said liquid phase isomerizationunit.